Method for producing 2-chloro-3,3,3-trifluoropropene and facility for implementing same

ABSTRACT

The present invention relates to a process for producing 2-chloro-3,3,3-trifluoropropene, comprising the steps: i) providing a stream A comprising at least one chlorinated compound selected from the group consisting of 2,3-dichloro-1,1,1-trifluoropropane, 1,1,1,2,3-pentachloropropane, 1,1,2,3-tetrachloropropene and 2,3,3,3-tetrachloropropene; and ii) in an adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing said stream A into contact, in the presence or absence of a catalyst, with HF in order to produce a stream B comprising 2-chloro-3,3,3-trifluoropropene, characterized in that the temperature at the inlet of the fixed bed of said adiabatic reactor is between 300° C. and 400° C. and the longitudinal temperature difference between the inlet of the fixed bed and the outlet of the fixed bed of said reactor is less than 20° C.

TECHNICAL FIELD OF THE INVENTION

The present invention relates to the production of hydrofluoroolefins, in particular the present invention relates to the production of 2-chloro-3,3,3-trifluoropropene.

TECHNOLOGICAL BACKGROUND OF THE INVENTION

Halogenated hydrocarbons, in particular fluorinated hydrocarbons, such as hydrofluoroolefins, are compounds having a structure which is useful as functional materials, solvents, refrigerants, blowing agents and monomers for functional polymers or starting materials for such monomers. Hydrofluoroolefins, such as 2,3,3,3-tetrafluoropropene (HFO-1234yf), are attracting attention because they offer a promising behavior as refrigerants having a low global warming potential.

Processes for the production of fluoroolefins are usually carried out in the presence of a starting substance, such as a chlorine-containing alkane or a chlorine-containing alkene, and in the presence of a fluorinating agent, such as hydrogen fluoride. These processes may be performed in the gas phase or in the liquid phase, in the absence or presence of a catalyst. For example, US 2009/0240090 discloses a gas-phase process for the preparation of 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf) from 1,1,1,2,3-pentachloropropane (HCC-240db). The HCFO-1233xf thus produced is converted into 2-chloro-1,1,1,2-tetrafluoropropane (HCFC-244bb) in the liquid phase and then the latter is converted into 2,3,3,3-tetrafluoropropene.

WO 2013/088195 also discloses a process for the preparation of 2,3,3,3-tetrafluoropropene from 1,1,1,2,3-pentachloropropane and/or 1,1,2,2,3-pentachloropropane, comprising the steps: (a) catalytic reaction of 1,1,1,2,3-pentachloropropane and/or 1,1,2,2,3-pentachloropropane with HF to give a reaction mixture comprising HCl, 2-chloro-3,3,3-trifluoropropene, 2,3,3,3-tetrafluoropropene, unreacted HF and possibly 1,1,1,2,2-pentafluoropropane; (b) separating the reaction mixture into a first stream comprising HCl and 2,3,3,3-tetrafluoropropene and a second stream comprising HF, 2-chloro-3,3,3-trifluoropropene and possibly 1,1,1,2,2-pentafluoropropane; (c) catalytic reaction of said second stream to give a reaction mixture comprising 2,3,3,3-tetrafluoropropene, HCl, unreacted 2-chloro-3,3,3-trifluoropropene, unreacted HF and possibly 1,1,1,2,2-pentafluoropropane; and (d) supplying the reaction mixture obtained in step c) directly to step a) without separation.

In processes for producing 2,3,3,3-tetrafluoropropene, the mastering and control of the reaction temperature is an important parameter which makes it possible to achieve the desired reaction kinetics, conversions and selectivities. This is also particularly recommended to avoid thermal decompositions of thermally sensitive compounds which can impact the activity of the catalyst through the formation of coke and thus considerably reduce the service life of the catalyst.

It is known from WO 2008/054781 that one temperature (300-350° C.) promotes formation of 1234yf, 245cb and 1233xf, while a higher temperature (350-450° C.) promotes formation of the isomers 1234ze, 245fa and 1233zd.

It is therefore important to master and control the temperature of the gases at the inlet of the reactors but also to master and control at all points of the catalytic mass, if there is one.

A multitubular reactor is by definition the ideal isothermal reactor for being able to control the reaction temperature and obtaining the most uniform reaction temperature possible since the catalyst is distributed in tubes and a fluid can circulate in the grille around the tubes to either remove reaction heat in the event of an exothermic reaction, or add heat in the event of an endothermic reaction. On the other hand, when large amounts of catalysts have to be used, the production of a multitubular reactor may prove to be impossible because it would take too many tubes and a homogeneous distribution of the gases in each of the tubes then proves to be very difficult to achieve. In addition, the maintenance of large multitubular reactors proves to be much more difficult and expensive; in particular, the catalyst change operations require lengthy immobilization of the reactor, both to drain the spent catalyst and to fill each tube extremely uniformly with new catalyst. This negative aspect will be reinforced when the service life of the catalyst is short.

Consequently, the use of an adiabatic fixed bed reactor is preferred. Nevertheless, this type of reactor does not exhibit heat exchange with an external environment by definition. Indeed, the adiabatic reactor is characterized by a non-homogeneous temperature at any point of the fixed bed and thus, by a temperature gradient that is both radial and longitudinal, due to the reaction heats and thermal losses at the outer walls of the reactor.

Document US 2016/0347692 describes the implementation of a process for the radical production in a homogeneous gas phase of chlorinated or fluorinated propene in an adiabatic flow reactor controlling the turbulence of the streams entering the reactor.

There is nevertheless a need to improve the processes for producing 2-chloro-3,3,3-trifluoropropene in adiabatic reactors.

SUMMARY OF THE INVENTION

According to a first aspect, the present invention relates to a process for producing 2-chloro-3,3,3-trifluoropropene, comprising the steps:

i) providing a stream A comprising at least one chlorinated compound selected from the group consisting of 2,3-dichloro-1,1,1-trifluoropropane, 1,1,1,2,3-pentachloropropane, 1,1,2,3-tetrachloropropene and 2,3,3,3-tetrachloropropene; and

ii) in an adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing said stream A into contact, in the presence or absence of a catalyst, with HF in order to produce a stream B comprising 2-chloro-3,3,3-trifluoropropene,

characterized in that the temperature at the inlet of the fixed bed of said adiabatic reactor is between 300° C. and 400° C. and the longitudinal temperature difference between the inlet of the fixed bed and the outlet of the fixed bed of said reactor is less than 20° C.

The value of the longitudinal temperature difference is considered as an absolute value.

According to one preferred embodiment, the temperature at the inlet of the fixed bed of said reactor is between 340° C. and 380° C. and the longitudinal temperature difference between the inlet of the fixed bed of said reactor and the outlet of the fixed bed of said reactor is less than 20° C.

According to one preferred embodiment, in step ii), the HF/chlorinated compounds molar ratio is adjusted so as to keep the longitudinal temperature difference between the inlet of the fixed bed and the outlet of the fixed bed of the reactor less than 20° C.

According to one preferred embodiment, in step ii), the HF/chlorinated compounds molar ratio is greater than or equal to 5, advantageously greater than or equal to 10, preferably greater than or equal to 12.

According to one preferred embodiment, said reactor comprises side walls comprising an inner layer, an intermediate layer placed on said inner layer and an insulating layer placed on said intermediate layer; and the radial temperature difference between a point located at the center of the fixed bed of said reactor and a point located in the radial plane at the level of the inner layer of the side wall of said reactor is less than 10° C. Said inner layer is that which is in contact with the reagents. The value of the radial temperature difference is considered as an absolute value.

According to one preferred embodiment, said reactor comprises side walls comprising an inner layer, an intermediate layer placed on said inner layer and an insulating layer placed on said intermediate layer; said insulating layer being made of a heat-insulating material M2, the thickness of which ranges between 1 mm and 500 mm.

According to one preferred embodiment, the heat-insulating material M2 is selected from the group consisting of rock wool, glass wool, silicate fibers, calcium-magnesium silicates, calcium silicates, microporous insulators, cellular glass, expanded perlite and exfoliated vermiculite.

According to one preferred embodiment, the pressure at the inlet of said reactor is between 3 and 15 bara.

According to one preferred embodiment, at least one portion of said stream B is recycled to step i) and said at least one portion of said stream B that has been recycled has an electrical conductivity of less than 15 mS/cm.

According to a second aspect, the present invention relates to a facility for producing 2-chloro-3,3,3-trifluoropropene, comprising:

-   -   an adiabatic reactor comprising a bottom, a cover and side walls         joining the bottom and the cover, at least one fixed bed and at         least one rod supporting one or more temperature sensor(s); said         bottom, said cover and said side walls each comprise at least an         inner layer, an intermediate layer placed on said inner layer         and an insulating layer placed around said intermediate layer;         said inner layer being made of a material M1 comprising a nickel         mass content of at least 30%; said intermediate layer being made         of a material M1′ comprising at least 70% by weight of iron;         said insulating layer being made of a heat-insulating material         M2 selected from the group consisting of rock wool, glass wool,         silicate fibers, calcium-magnesium silicates, calcium silicates,         microporous insulators, cellular glass, expanded perlite and         exfoliated vermiculite; the length of said at least one rod         supporting one or more temperature sensor(s) being at least         equal to the height of said fixed bed; and said at least one rod         comprising at least one temperature sensor placed in said fixed         bed;     -   a system for feeding said reactor with reaction stream         comprising a supply line for hydrofluoric acid and at least one         supply line for a stream A comprising at least one of the         chlorinated compounds selected from the group consisting of         2,3-dichloro-1,1,1-trifluoropropane,         1,1,1,2,3-pentachloropropane, 1,1,2,3-tetrachloropropene and         2,3,3,3-tetrachloropropene;     -   a system for collecting and purifying the outlet stream from         said reactor;     -   at least one conductivity meter capable of measuring the         electrical conductivity of the reaction stream entering said         reactor.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 schematically represents a reactor according to one particular embodiment of the present invention.

FIG. 2 schematically represents a view in longitudinal section of a reactor according to one particular embodiment of the present invention.

FIG. 3 schematically represents a view in transverse section of a reactor according to one particular embodiment of the present invention.

FIG. 4 schematically represents a sectional view of the side walls of a reactor according to one particular embodiment of the present invention.

FIG. 5 schematically represents a facility for producing 2,3,3,3-tetrafluoropropene according to one particular embodiment of the present invention.

DETAILED DESCRIPTION OF THE INVENTION

The present invention relates to a process for producing 2-chloro-3,3,3-trifluoropropene. Preferably, said process for producing 2-chloro-3,3,3-tetrafluoropropene comprises the steps:

i) providing a stream A comprising at least one of the chlorinated compounds selected from the group consisting of 2,3-dichloro-1,1,1-trifluoropropane, 1,1,1,2,3-pentachloropropane, 1,1,2,3-tetrachloropropene and 2,3,3,3-tetrachloropropene; and

ii) in an adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing said stream A into contact, in the presence or absence of a catalyst, with HF in order to produce a stream B comprising 2-chloro-3,3,3-trifluoropropene.

Preferably, the temperature at the inlet of the fixed bed of said reactor is between 300° C. and 400° C. and the longitudinal temperature difference between the inlet of the fixed bed and the outlet of the fixed bed of the reactor is less than 20° C.

Preferably, the temperature at the inlet of the fixed bed of said reactor is between 330° C. and 400° C., preferably between 330° C. and 390° C., in particular between 340° C. and 380° C. In this step ii), a temperature above 400° C. can render the catalyst irreversibly inactive, while a temperature below 300° C. prevents the fluorination reaction from being carried out.

As mentioned above, in an adiabatic reactor, the temperature within the reactor, and in particular within the fixed bed, varies longitudinally, i.e. the temperature varies between the inlet of the reactor and the outlet of the reactor, in particular between the inlet of the fixed bed and the outlet of the fixed bed. FIG. 2 represents a schematic view in longitudinal section of a reactor 1 according to one particular embodiment of the present invention and comprising a fixed bed 5. The longitudinal temperature difference ΔTa is defined by the temperature difference between the inlet of the fixed bed 9 and the outlet of the fixed bed 10.

Preferably, the longitudinal temperature difference between the inlet of the fixed bed of said reactor and the outlet of the fixed bed of said reactor is less than 20° C., advantageously less than 19° C., preferably less than 18° C., more preferentially less than 17° C., in particular less than 16° C., more particularly less than 15° C., preferably less than 14° C., advantageously preferably less than 13° C., preferentially preferably less than 12° C., more preferentially preferably less than 11° C., particularly preferably less than 10° C.

According to a preferred embodiment, step ii) is carried out in the presence of a catalyst, preferably a chromium-based catalyst. Preferably, the chromium-based catalyst may be a chromium oxide (for example CrO₂, CrO₃ or Cr₂O₃), a chromium oxyfluoride or a chromium fluoride (for example CrF₃) or a mixture thereof. The chromium oxyfluoride may have a fluorine content of between 1% and 60% by weight on the basis of the total weight of the chromium oxyfluoride, advantageously between 5% and 55% by weight, preferably between 10% and 52% by weight, more preferentially between 15% and 52% by weight, in particular between 20% and 50% by weight, more particularly between 25% and 45% by weight, favorably between 30% and 45% by weight, more favorably from 35% to 45% by weight of fluorine on the basis of the total weight of chromium oxyfluoride. The catalyst can also comprise a cocatalyst chosen from the group consisting of Ni, Co, Zn, Mg, Mn, Fe, Zn, Ti, V, Zr, Mo, Ge, Sn, Pb and Sb; preferably Ni, Co, Zn, Mg and Mn; in particular Ni, Co and Zn. The content by weight of the cocatalyst is between 1% and 10% by weight, based on the total weight of the catalyst. The catalyst may or may not be supported. A support, such as alumina, for example in its a form, activated alumina, aluminum halides (AlF₃, for example), aluminum oxyhalides, activated carbon, magnesium fluoride or graphite, can be used.

Preferably, the catalyst can a specific surface area of between 1 and 100 m²/g, preferably between 5 and 80 m²/g, more preferentially between 5 and 70 m²/g, ideally between 5 and 50 m²/g, in particular between 10 and 50 m²/g, more particularly between 15 and 45 m²/g.

According to another preferred embodiment, step ii) is carried out in the absence of catalyst. In this case, said fixed bed contains an inert solid. The inert solid can be corundum, silicon carbide, quartz balls or rings, a metallic packing made of a metal M1 as defined in the present application or nickel balls. According to a preferred embodiment, step ii) is carried out at atmospheric pressure or at a pressure greater than atmospheric pressure, advantageously at a pressure of greater than 1.5 bara, preferably at a pressure of greater than 2.0 bara, in particular at a pressure of greater than 2.5 bara, more particularly at a pressure of greater than 3.0 bara. Preferably, step ii) is carried out at a pressure of between atmospheric pressure and 20 bara, preferably between 2 and 18 bara, more preferentially between 3 and 15 bara. Preferably, step ii) of the present process is performed with a contact time of between 1 and 100 seconds, preferably between 2 and 75 seconds, in particular between 3 and 50 seconds. An oxidant, such as oxygen or chlorine, may be added during step ii). The molar ratio of the oxidant to the hydrocarbon compound can be between 0.005 and 2, preferably between 0.01 and 1.5. The oxidant can be pure oxygen, air or a mixture of oxygen and nitrogen.

Preferably, in step ii), the HF/said at least one chlorinated compound molar ratio is greater than or equal to 5, advantageously greater than or equal to 10, preferably greater than or equal to 12. Advantageously, the HF/said at least one chlorinated compound molar ratio is between 12:1 and 150:1, preferably between 12:1 and 125:1, more preferably between 12:1 and 100:1.

As mentioned above, in an adiabatic reactor, the temperature within the reactor, and in particular within the fixed bed, varies radially, i.e. the temperature varies between the center of the reactor and the side walls of the reactor located in the same plane, in particular between the center of the fixed bed and the side wall of the reactor located in the same plane.

The control of the radial temperature in the fixed bed can be carried out by insulating the side walls of said reactor with a heat-insulating material of a defined thickness. Thus, said side walls each comprise at least one inner layer and an insulating layer placed around said inner layer. Preferably, an intermediate layer is placed between said inner layer and said insulating layer.

FIG. 3 represents a transverse view along the sectional plane (a,a′) of a reactor 1 according to one embodiment of the present invention and comprising a fixed bed 5. The side walls 3 of said reactor comprise an inner layer 21, an intermediate layer 22 placed on said inner layer 21 and an insulating layer 23 placed on said intermediate layer 22 (FIG. 4). The radial temperature difference ΔTb is defined by the difference between a point located at the center of the fixed bed 5 of the reactor and a point 12 located in the radial plane at the level of the inner layer 21 of the side wall 3 of said reactor (FIG. 3).

Thus, the radial temperature difference between a point located at the center of the fixed bed of the reactor and a point located in the radial plane at the level of the inner layer of the side wall of said reactor is less than 10° C., advantageously less than 9° C., preferably less than 8° C., more preferentially less than 7° C., in particular less than 6° C., more particularly less than 5° C.

According to one preferred embodiment, said inner layer has a thickness of between 0.01 and 20 mm. Preferably, said inner layer can have a thickness of between 0.05 and 15 mm, preferably between 0.1 and 10 mm, more preferentially between 0.1 and 5 mm.

Said inner layer can be made of a material M1 comprising a nickel mass content of at least 30%. Advantageously, the material M1 comprises at least 40% by weight of nickel on the basis of the total weight of the material M1. Preferably, the material M1 comprises at least 45% by weight of nickel, more preferentially at least 50% by weight of nickel, in particular at least 55% by weight of nickel, more particularly at least 60% by weight of nickel, favorably at least 65% by weight of nickel, more favorably at least 70% by weight of nickel on the basis of the total weight of the material M1. The material M1 may also comprise chromium in a content of less than 35% by weight on the basis of the total weight of the material M1, advantageously less than 30% by weight, preferably less than 20% by weight, more preferentially less than 15% by weight, in particular less than 10% by weight, more particularly less than 5% by weight on the basis of the total weight of the material M1. The material M1 may also comprise molybdenum in a content of less than 35% by weight on the basis of the total weight of the material M1, advantageously less than 30% by weight, preferably less than 20% by weight, more preferentially less than 15% by weight, in particular less than 10% by weight, more particularly less than 5% by weight on the basis of the total weight of the material M1. Preferably, the material M1 comprises at least 40% by weight of nickel on the basis of the total weight of the material M1, preferably at least 45% by weight of nickel, more preferentially at least 50% by weight of nickel, in particular at least 55% by weight of nickel, more particularly at least 60% by weight of nickel, favorably at least 65% by weight of nickel, more favorably at least 70% by weight of nickel on the basis of the total weight of the material M1; and less than 35% by weight of chromium, advantageously less than 30% by weight, preferably less than 20% by weight, more preferentially less than 15% by weight, in particular less than 10% by weight, more particularly less than 5% by weight of chromium on the basis of the total weight of the material M1; and less than 35% by weight of molybdenum, advantageously less than 30% by weight, preferably less than 20% by weight, more preferentially less than 15% by weight, in particular less than 10% by weight, more particularly less than 5% by weight of molybdenum on the basis of the total weight of the material M1. The material M1 may also comprise cobalt in a content of less than 10% by weight on the basis of the total weight of the material M1, advantageously less than 8% by weight, preferably less than 6% by weight, more preferentially less than 4% by weight, in particular less than 3% by weight, more particularly less than 2% by weight on the basis of the total weight of the material M1. The material M1 may also comprise tungsten in a content of less than 10% by weight on the basis of the total weight of the material M1, advantageously less than 9% by weight, preferably less than 8% by weight, more preferentially less than 7% by weight, in particular less than 6% by weight, more particularly less than 5% by weight on the basis of the total weight of the material M1. The material M1 may also comprise iron in a content of less than 25% by weight on the basis of the total weight of the material M1, advantageously less than 20% by weight, preferably less than 15% by weight, more preferentially less than 10% by weight, in particular less than 7% by weight, more particularly less than 5% by weight on the basis of the total weight of the material M1. The material M1 may also comprise manganese in a content of less than 5% by weight on the basis of the total weight of the alloy, advantageously less than 4% by weight, preferably less than 3% by weight, more preferentially less than 2% by weight, in particular less than 1% by weight, more particularly less than 0.5% by weight on the basis of the total weight of the material M1. The material M1 may also comprise copper in a content of less than 50% by weight, advantageously less than 45% by weight, preferably less than 40% by weight, more preferentially less than 35% by weight, in particular less than 30% by weight, more particularly less than 25% by weight of copper on the basis of the total weight of the material M1.

According to one preferred embodiment, said intermediate layer has a thickness of between 0.1 and 50 mm. Preferably, said intermediate layer may have a thickness of between 0.5 and 40 mm, preferably between 1 and 30 mm, more preferentially between 1 and 25 mm. According to one preferred embodiment, said intermediate layer 22 is placed between said inner layer 21, in contact with the reagents, and said insulating layer 23 (FIG. 4). Said intermediate layer 22 may be made of a material M1′. According to a preferred embodiment, the material M1′ comprises at least 70% by weight of iron, advantageously at least 75% by weight, preferably at least 80% by weight, more preferentially at least 85% by weight, in particular at least 90% by weight, more particularly at least 95% by weight of iron on the basis of the total weight of the material M1′. The material M1′ may also comprise less than 2% by weight of carbon, advantageously less than 1.5% by weight, preferably less than 1% by weight, more preferentially less than 0.75% by weight, in particular less than 0.5% by weight, more particularly less than 0.2% by weight, favorably less than 0.1% by weight on the basis of the total weight of the material M1′. More particularly, the material M1′ may comprise between 0.01% and 0.2% by weight of carbon on the basis of the total weight of the material M1′. The material M1′ may also comprise less than 2% by weight of molybdenum, advantageously less than 1.5% by weight, preferably less than 1.25% by weight, more preferentially less than 1% by weight of molybdenum on the basis of the total weight of the material M1′. More particularly, the material M1′ may comprise between 0.1% and 1% by weight of molybdenum on the basis of the total weight of the material M1′. The material M1′ may also comprise less than 5% by weight of chromium, advantageously less than 4% by weight, preferably less than 3% by weight, more preferentially less than 2% by weight, in particular less than 1% by weight of chromium on the basis of the total weight of the material M1′. More particularly, the material M1′ may comprise between 0.5% and 2% by weight of chromium on the basis of the total weight of the material M1′. The material M1′ may also comprise less than 2% by weight of silicon, advantageously less than 1.5% by weight, preferably less than 1.25% by weight, more preferentially less than 1% by weight of silicon on the basis of the total weight of the material M1′. More particularly, the material M1′ may comprise between 0.1% and 1.5% by weight of silicon on the basis of the total weight of the material M1′. The material M1′ may also comprise less than 2% by weight of manganese, advantageously less than 1.5% by weight, preferably less than 1.25% by weight, more preferentially less than 1% by weight of manganese on the basis of the total weight of the material M1′. More particularly, the material M1′ may comprise between 0.1% and 1% by weight of manganese on the basis of the total weight of the material M1′.

Preferably, said insulating layer is made of a heat-insulating material M2. Said heat-insulating material M2 is selected from the group consisting of rock wool, glass wool, silicate fibers, calcium-magnesium silicates, calcium silicates, microporous insulators, cellular glass, expanded perlite and exfoliated vermiculite. The silicate fibers include, for example, aluminosilicate fibers. In particular, the side walls of said reactor comprise an insulating layer made of a heat-insulating material M2, the thickness of which ranges between 1 mm and 500 mm, preferably between 5 mm and 400 mm.

According to a preferred embodiment, the pressure at the inlet of said reactor is atmospheric pressure or a pressure greater than this; advantageously, the pressure at the inlet of said reactor is greater than 1.5 bara, preferably greater than 2.0 bara, in particular greater than 2.5 bara, more particularly greater than 3.0 bara. Preferably, step ii) is carried out at a pressure at the inlet of said reactor of between atmospheric pressure and 20 bara, preferably between 2 and 18 bara, more preferentially between 3 and 15 bara.

According to a preferred embodiment, said at least one chlorinated compound and HF are brought into contact prior to the entry of these into said reactor. The resulting mixture is the mixture C.

Preferably, said at least one chlorinated compound is in the liquid state. The latter is vaporized by mixing with the HF. The resulting mixture C is then in gaseous form. In particular, the mixing between HF and said at least one chlorinated compound is carried out in a static mixer. Preferably, said at least one chlorinated compound is introduced into the static mixer via one or more spray nozzles. Said at least one chlorinated compound is thus sprayed in the form of droplets before being vaporized by mixing with HF, thus forming a mixture C in gaseous form. The spraying of said at least one chlorinated compound in the form of fine droplets makes it possible to ensure a more efficient vaporization of this compound. For example, the mean diameter of the droplets thus produced can be less than 500 μm.

Said mixture C can optionally be heated or cooled before it is introduced into said reactor. This step can be carried out via a heat exchanger in order to control the temperature at the inlet of said reactor.

According to a preferred embodiment, said stream B comprises 2-chloro-3,3,3-trifluoropropene, HF and HCl and optionally said at least one unreacted chlorinated compound. The stream B can be purified, preferably by distillation, in order to isolate the 2-chloro-3,3,3-trifluoropropene.

According to a particular embodiment, the stream B comprises, in addition to 2-chloro-3,3,3-trifluoropropene, HCl and HF, 2,3,3,3-tetrafluoropropene. The stream B can optionally comprise 2,3-dichloro-3,3-difluoropropene, 2,3,3-trichloro-3-fluoropropene and/or 1,1,1,2,2-pentafluoropropane.

According to a preferred embodiment, the stream B is purified, preferably by distillation, so as to form a first stream comprising 2,3,3,3-tetrafluoropropene, HCl and optionally 1,1,1,2,2-pentafluoropropane, and a second stream comprising HF and 2-chloro-3,3,3-trifluoropropene and optionally 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene. In particular, the distillation can be carried out at a pressure of from 1 to 20 bara, preferably from 2 to 18 bara, more particularly at a pressure of from 3 to 15 bara. In particular, the temperature at the top of the distillation column is from −85° C. to −10° C., preferably from −60° C. to −20° C.

Alternatively, the stream B is purified, preferably by distillation, so as to form a stream comprising HCl, 2-chloro-3,3,3-trifluoropropene, 2,3,3,3-tetrafluoropropene and optionally 1,1,1,2,2-pentafluoropropane and a stream comprising HF and optionally 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene. In this alternative embodiment, the stream comprising hydrofluoric acid and optionally 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene can be recycled to step ii) of the present process.

According to a preferred embodiment, said stream B obtained in step ii) is cooled prior to the abovementioned purification. In particular, said stream B obtained in step ii) is cooled to a temperature of less than 100° C., then distilled in order to form said first stream comprising 2,3,3,3-tetrafluoropropene, HCl and optionally 1,1,1,2,2-pentafluoropropane and said second stream comprising HF and 2-chloro-3,3,3-trifluoropropene and optionally 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene; the temperature at the distillation column top is from −60° C. to −20° C. and the distillation is carried out at a pressure from 3 to 15 bara.

Said stream B can be cooled, before distillation, to a temperature of less than 95° C., advantageously of less than 90° C., preferably of less than 85° C., more preferentially of less than 80° C., in particular of less than 70° C., more particularly of less than 60° C., favorably of less than 55° C., advantageously favorably of less than 50° C., preferentially favorably of less than 40° C., more preferentially favorably of less than 30° C., particularly favorably of less than 25° C., more particularly favorably of less than 20° C. The cooling of the stream of products obtained to such temperatures can facilitate the subsequent distillation.

The cooling of said stream B can be carried out by virtue of one or a plurality of heat exchangers. The cooling of said stream B can be carried out by passing the latter through one, two, three, four, five, six, seven, eight, nine or ten heat exchangers; preferably, the number of heat exchangers is between 2 and 8, in particular between 3 and 7.

Said second stream comprising HF and 2-chloro-3,3,3-trifluoropropene and optionally 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene can be purified, preferably by distillation, so as to form a third stream comprising hydrofluoric acid and optionally 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene, and a fourth stream comprising at least 95% by weight of 2-chloro-3,3,3-trifluoropropene, preferably at least 98% by weight of 2-chloro-3,3,3-trifluoropropene on the basis of the total weight of said fourth stream.

The third stream comprising hydrofluoric acid and optionally 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene can be recycled to step ii) of the present process. In this case, said third stream is mixed with hydrofluoric acid before being used in step ii) of the present process.

Preferably, the process according to the present invention is carried out continuously.

Preferably, the process is carried out continuously and in the gas phase.

Preferably, said stream A has an electrical conductivity of less than 15 mS/cm. Advantageously, the electrical conductivity of said stream A is less than 14 mS/cm, preferably less than 13 mS/cm, more preferentially less than 12 mS/cm, in particular less than 11 mS/cm, more particularly less than 10 mS/cm, more preferably less than 9 mS/cm, advantageously preferably less than 8 mS/cm, preferentially preferably less than 7 mS/cm, more preferentially preferably less than 6 mS/cm, particularly preferably less than 5 mS/cm. Preferably, step ii) is carried out in the presence of hydrofluoric acid having an electrical conductivity of less than 10 mS/cm, preferably less than 5 mS/cm. Preferably, the electrical conductivity of the third stream that can be recycled to step ii) is less than 15 mS/cm, advantageously less than 10 mS/cm, preferably less than 5 mS/cm.

The electrical conductivity of said stream A or of HF or of the third stream or of the stream comprising HF in the embodiment described above is measured prior to step i) or ii). Preferably, the electrical conductivity is measured when the stream in question or the HF is in liquid form. Said process according to the present invention can therefore comprise a step of heating the stream in question or the HF prior to carrying out step i) in order to provide said stream A in gaseous form. Preferably, said stream A used in step i) is in gaseous form when it is brought into contact with HF. The electrical conductivity is measured at ambient temperature. The electrical conductivity is measured using an inductive conductivity measurement cell according to the practice known to those skilled in the art. Preferably, the measurement cell is coated with a material resistant to a corrosive medium, in particular resistant to hydrofluoric acid. The electrical conductivity of a stream can be reduced, in order to achieve a conductivity of less than 15 mS/cm, by reducing the concentration of electrolyte possibly present in the stream according to techniques known to those skilled in the art (distillation, cooling and separation by settling, passage through 3 to 5 Å molecular sieves or zeolites). Such an electrical conductivity makes it possible to improve the conversion and/or the selectivity of the reaction.

According to a second aspect of the present invention, an adiabatic reactor 1 is provided. Preferably, said reactor 1 comprises a bottom 4, a cover 2 and side walls 3 joining the bottom 4 and the cover 2, at least one fixed bed 5 and at least one rod 6 supporting one or more temperature sensors 7 a, 7 b (FIG. 1).

Preferably, said bottom 4, said cover 2 and said side walls 3 each comprise at least one inner layer 21, an intermediate layer 22 placed on said inner layer and an insulating layer 23 placed around said intermediate layer 22. Said inner layer 21, intermediate layer 22 and insulating layer 23 are respectively made of a material M1, M1′ and M2 as described above.

According to one preferred embodiment, said insulating layer 23 may be covered by a base layer 24. Thus, said insulating layer 23 is placed between said intermediate layer 22 and said base layer 24 (FIG. 4). Said base layer 24 may be made of a material M3. Said material M3 can be a metallic coating made with sheets of aluminum, stainless steel or galvanized steel. Preferably, said base layer has a thickness of between 0.2 mm and 2 mm.

Said inner layer 21, said intermediate layer 22, said insulating layer 23 and said base layer 22 can be placed one on top of the other according to techniques well known to those skilled in the art.

Preferably, the length of said at least one rod 6 is at least equal to the height of said fixed bed 5. In particular, said at least one rod 6 comprises at least one temperature sensor or at least two temperature sensors or at least 3 temperature sensors, advantageously at least 5 temperature sensors, preferably at least 7 temperature sensors, in particular at least 10 temperature sensors, preferably at least 12 temperature sensors, preferentially preferably at least 15 temperature sensors.

Preferably, at least one of said one or more temperature sensors, supported by said at least one rod, is placed in said fixed bed 5. In particular, at least two or three or four or five or six or seven temperature sensors, supported by said at least one rod, are arranged in said fixed bed 5.

Preferably, each rod 6 can comprise either an identical number or a different number of temperature sensors. In particular, each rod can comprise a temperature sensor in the headspace and/or in the bottom of the reactor (FIG. 1, reference 7 b and 7 b′). Likewise, the temperature sensors 7 a, 7 b can be distributed equidistantly or in a more targeted manner as required for controlling the temperature profile in the fixed bed.

Preferably, said reactor can comprise at least two rods 6, more preferentially at least three rods 6, in particular at least four rods 6. In particular, said reactor may comprise between 1 and 20 rods 6, advantageously between 2 and 15 rods 6, preferably between 3 and 10 rods 6.

Preferably, the reactor 1 is fed with hydrocarbon compound 14 via feed lines 13. The reactor also comprises effluent or outlet lines 15 for removing the reaction mixture 16 from the reactor (FIG. 1).

Preferably, the feed or outlet lines of the reactor are made of material capable of also resisting corrosion, for example made of the material M1 covered with a layer of material M2 and a base layer made of a material M3. The feed lines may be of tubular shape. Alternatively, the feed or outlet lines may comprise an inner layer, preferably made of a material M1 as described above, an insulating layer, preferably made of a material M2 as described above, and a base layer, preferably made of a material M3 as described above. The reactor also comprises one or more dephlegmator(s), one or more dip tube(s), one or more device(s) for introducing the raw materials, and one or more grating(s) for supporting and retaining the catalyst. Said one or more dephlegmator(s) and/or said one or more dip tube(s) and/or said one or more device(s) for introducing the raw materials and/or said one or more grating(s) for supporting and retaining the catalyst may comprise an inner layer, preferably made of a material M1 as described above.

Preferably, the fixed bed 5 comprises a catalyst or an inert solid or both. The inert solid can be corundum, silicon carbide, quartz balls or rings, a metallic packing made of a metal M1 as defined in the present application or nickel balls. Preferably, when the fixed bed 5 comprises a catalyst, the inert solid is placed in the upper part 17 and the lower part 18 of the fixed bed 5, said catalyst 19 c being located between the layers of the inert solid 19 a and 19 b, in the central part 20 of the fixed bed 5. In an alternative embodiment, when the fixed bed 5 comprises a catalyst, the inert solid is placed in the upper part 17 or in the lower part 18 of the fixed bed 5. In an alternative embodiment, when the fixed bed 5 comprises a catalyst, no layer of inert solid is placed in the fixed bed. In an alternative embodiment, wherein the reactor does not contain a catalyst, the lower part 18, the central part 20 and the upper part 17 of the fixed bed 5 may contain only inert solid. This alternative embodiment can be implemented when, for example, step ii) of the process according to the present invention is carried out in the absence of a catalyst. In this case, the inert solid makes it possible to improve the distribution of gases inside the reactor. Preferably, the inert solid is corundum or nickel balls.

Preferably, the fixed bed 5 contains a catalyst layer 19 c in its central part 20. In one preferred embodiment, the catalyst is distributed homogeneously in the fixed bed. The homogeneous distribution of the catalyst in the fixed bed makes it possible to minimize disruptions in the gas flow and to avoid hot spots within the catalyst layer. The presence of hot spots can lead to irreversible crystallization of the catalyst causing deactivation thereof. The loading of the fixed bed is carried out according to the specific method of dense loading of the catalyst. This method is known to those skilled in the art. It makes it possible to obtain an optimal distribution of the catalyst inside the reactor by avoiding channeling during the reaction and the attrition of the catalyst. In general, the apparent density by weight of the catalyst in the fixed bed is greater than the theoretical density by weight thereof. The apparent density by weight is determined according to ASTM D1895.

Preferably, said reactor is a gas-phase fluorination reactor.

The present invention makes it possible to implement a process for producing 2-chloro-3,3,3-trifluoropropene with a larger amount of catalyst, if said process is carried out in the presence of catalyst. In addition, the radial and longitudinal mastering and control of the temperature make it possible to maintain reaction conversion and selectivity.

According to a third aspect of the invention, a facility for producing 2-chloro-3,3,3-trifluoropropene is provided. Preferably, the facility comprises an adiabatic reactor 101 according to the present invention, a system for feeding said reactor with reaction stream, a system for collecting and purifying the outlet stream 105 from said reactor. Preferably, said facility also comprises at least one conductivity meter 121 capable of measuring the electrical conductivity of the reaction stream entering said reactor.

Preferably, said facility also comprises a heat exchanger 106 fed with the outlet stream 105 and connected to a first distillation column 108. Preferably, said facility also comprises a compressor 110 fed with the stream coming from said first distillation column 108. Preferably, said facility comprises a second distillation column 112 fed with a stream coming from the compressor 110. Said second distillation column 112 aims to remove all or a portion of the HCl present in the stream conveyed to it. Said facility may also comprise a plurality of other distillation columns for purifying the 2,3,3,3-tetrafluoropropene if the latter is present in the outlet stream 105.

A facility according to one particular embodiment of the present invention is illustrated in FIG. 5. The system for feeding the reactor 101 with reaction stream comprises a supply line for hydrofluoric acid 102, 120 and a supply line for said chlorinated compound 103 and a device 104 for mixing the hydrofluoric acid and said chlorinated compound. Said mixing device 104 is preferably a static mixer. Thus, the hydrofluoric acid and said chlorinated compound are mixed, pulverized and vaporized in said mixing device 104 before being introduced into said reactor 101. Preferably, the outlet stream 105 from the reactor 101 comprises 2-chloro-3,3,3-trifluoropropene, HF, HCl, 2,3,3,3-tetrafluoropropene and optionally said unreacted chlorinated compound, 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene. The facility comprises a heat exchanger 106 able to cool the outlet stream 105 coming from said reactor 101 to form a cooled stream. The outlet stream 105 is conveyed to a cooling device 106. The outlet stream 105 is thus cooled to a temperature of 0° C. to 70° C. before being introduced into a distillation column 108 via a pipe 107. The distillation column 108 is configured so as to allow separation between, on the one hand, hydrochloric acid and 2,3,3,3-tetrafluoropropene and, on the other hand, hydrofluoric acid and 2-chloro-3,3,3-trifluoropropene and optionally said unreacted chlorinated compound, 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene. The stream comprising 2,3,3,3-tetrafluoropropene and hydrochloric acid is recovered at the top of distillation column 108 to be conveyed via a pipe 109 to a compressor 110. The compressor makes it possible to compress the stream comprising 2,3,3,3-tetrafluoropropene and hydrochloric acid to a pressure of between 10 and 25 bara. The stream thus compressed is conveyed by the pipe 111 to a second distillation column 112. Said distillation column is configured so as to separate, on one hand, 2,3,3,3-tetrafluoropropene and, on the other hand, hydrochloric acid. The hydrochloric acid is recovered at the top of the distillation column 112 to be conveyed to a purification device 116 by the pipe 115. The hydrochloric acid purification device 116 is a device known from the prior art, for example from WO 2015/079137. The 2,3,3,3-tetrafluoropropene is recovered at the bottom of the distillation column 112 so as to be conveyed by the pipe 113 to a purification device 114. The stream comprising HF and 2-chloro-3,3,3-trifluoropropene and optionally said unreacted chlorinated compound, 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene is recovered at the bottom of distillation column 108. This stream can be conveyed to a fluorination reactor or purified. FIG. 5 represents an embodiment in which this stream is purified. Said stream is thus conveyed by the pipe 117 to a distillation column 118. The stream 119 obtained and recovered at the top of the distillation column comprises 2-chloro-3,3,3-trifluoropropene. The stream recovered at the bottom of the distillation column 118 comprising HF and optionally said unreacted chlorinated compound, 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene, is recycled to the mixing device 104. The electrical conductivity of the stream thus recycled is measured by the conductivity meter 121′ before said stream is introduced into the mixing device 104. The facility can also comprise a conductivity meter 121″ and 121′″ for measuring the electrical conductivity respectively of the HF from the feed line 102 and of the chlorinated compound from the feed line 103, before said compounds are introduced into the mixing device 104. Alternatively, the stream recovered at the bottom of distillation column 118 and comprising HF and optionally said unreacted chlorinated compound, 2,3-dichloro-3,3-difluoropropene and 2,3,3-trichloro-3-fluoropropene, can be recycled to the reactor 101. 

1-10. (canceled)
 11. A process for producing 2-chloro-3,3,3-trifluoropropene, comprising the steps: i. providing a stream A comprising at least one chlorinated compound selected from the group consisting of 2,3-dichloro-1,1,1-trifluoropropane, 1,1,1,2,3-pentachloropropane, 1,1,2,3-tetrachloropropene and 2,3,3,3-tetrachloropropene; and ii. in an adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing said stream A into contact, in the presence or absence of a catalyst, with HF in order to produce a stream B comprising 2-chloro-3,3,3-trifluoropropene, wherein the temperature at the inlet of the fixed bed of said adiabatic reactor is between 300° C. and 400° C. and a longitudinal temperature difference between the inlet of the fixed bed and the outlet of the fixed bed of said reactor is less than 20° C.
 12. The process as claimed in claim 11, wherein the temperature at the inlet of the fixed bed of said reactor is between 340° C. and 380° C. and the longitudinal temperature difference between the inlet of the fixed bed of said reactor and the outlet of the fixed bed of said reactor is less than 20° C.
 13. The process as claimed in claim 11, wherein, in step ii), an HF/at least one chlorinated compound molar ratio is adjusted so as to keep the longitudinal temperature difference between the inlet of the fixed bed and the outlet of the fixed bed of the reactor less than 20° C.
 14. The process as claimed in claim 11, wherein, in step ii), an HF/at least one chlorinated compound molar ratio is greater than or equal to
 5. 15. The process as claimed in claim 11, wherein said reactor comprises side walls comprising an inner layer, an intermediate layer placed on said inner layer and an insulating layer placed on said intermediate layer; and wherein a radial temperature difference between a point located at a center of the fixed bed of said reactor and a point located in a radial plane at a level of the inner layer of the side wall of said reactor is less than 10° C.
 16. The process as claimed in claim 11, wherein said reactor comprises side walls comprising an inner layer, an intermediate layer placed on said inner layer and an insulating layer placed on said intermediate layer; said insulating layer being made of a heat-insulating material M2, the thickness of which ranges between 1 mm and 500 mm.
 17. The process as claimed in claim 11, wherein the heat-insulating material M2 is selected from the group consisting of rock wool, glass wool, silicate fibers, calcium-magnesium silicates, calcium silicates, microporous insulators, cellular glass, expanded perlite, and exfoliated vermiculite.
 18. The process as claimed in claim 11, wherein the pressure at the inlet of said reactor is between 3 and 15 bara.
 19. The process as claimed in claim 11, wherein at least one portion of said stream B is recycled to step i) and said at least one portion of said stream B that has been recycled has an electrical conductivity of less than 15 mS/cm.
 20. A facility for producing 2-chloro-3,3,3-trifluoropropene, comprising: an adiabatic reactor comprising a bottom, a cover and side walls joining the bottom and the cover, at least one fixed bed and at least one rod supporting one or more temperature sensor(s); said bottom, said cover and said side walls each comprise at least an inner layer, an intermediate layer placed on said inner layer and an insulating layer placed around said intermediate layer; said inner layer being made of a material M1 comprising a nickel mass content of at least 30%; said intermediate layer being made of a material M1′ comprising at least 70% by weight of iron; said insulating layer being made of a heat-insulating material M2 selected from the group consisting of rock wool, glass wool, silicate fibers, calcium-magnesium silicates, calcium silicates, microporous insulators, cellular glass, expanded perlite and exfoliated vermiculite; the length of said at least one rod supporting the one or more temperature sensor(s) being at least equal to a height of said at least one fixed bed; and said at least one rod comprising at least one of the one or more temperature sensors placed in said fixed bed; a system for feeding said reactor with a reaction stream comprising a supply line for hydrofluoric acid and at least one supply line for a stream A comprising at least one of the chlorinated compounds selected from the group consisting of 2,3-dichloro-1,1,1-trifluoropropane, 1,1,1,2,3-pentachloropropane, 1,1,2,3-tetrachloropropene and 2,3,3,3-tetrachloropropene; a system for collecting and purifying an outlet stream from said reactor; and at least one conductivity meter capable of measuring the electrical conductivity of the reaction stream entering said reactor. 